US5294420A - Process for the desulfurization and denitrification of a waste gas containing halogen-containing materials - Google Patents

Process for the desulfurization and denitrification of a waste gas containing halogen-containing materials Download PDF

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Publication number
US5294420A
US5294420A US07/942,829 US94282992A US5294420A US 5294420 A US5294420 A US 5294420A US 94282992 A US94282992 A US 94282992A US 5294420 A US5294420 A US 5294420A
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moving bed
bed
waste gas
carbonaceous adsorbent
adsorbent
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US07/942,829
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English (en)
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Yoshiro Ito
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J Power Entech Inc
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Mitsui Mining Co Ltd
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Assigned to ELECTRIC POWER DEVELOPMENT CO., LTD. reassignment ELECTRIC POWER DEVELOPMENT CO., LTD. ASSIGNMENT OF ASSIGNORS INTEREST (SEE DOCUMENT FOR DETAILS). Assignors: MITSUI MINING CO., LTD.
Assigned to J-POWER ENTECH, INC. reassignment J-POWER ENTECH, INC. ASSIGNMENT OF ASSIGNORS INTEREST (SEE DOCUMENT FOR DETAILS). Assignors: ELECTRIC POWER DEVELOPMENT CO., LTD.
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    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/46—Removing components of defined structure
    • B01D53/60—Simultaneously removing sulfur oxides and nitrogen oxides
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/34—Chemical or biological purification of waste gases
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/02—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography
    • B01D53/06—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography with moving adsorbents, e.g. rotating beds
    • B01D53/08—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography with moving adsorbents, e.g. rotating beds according to the "moving bed" method
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2253/00—Adsorbents used in seperation treatment of gases and vapours
    • B01D2253/10—Inorganic adsorbents
    • B01D2253/102—Carbon
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2257/00—Components to be removed
    • B01D2257/20—Halogens or halogen compounds
    • B01D2257/204—Inorganic halogen compounds
    • B01D2257/2045—Hydrochloric acid
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2257/00—Components to be removed
    • B01D2257/20—Halogens or halogen compounds
    • B01D2257/204—Inorganic halogen compounds
    • B01D2257/2047—Hydrofluoric acid
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2257/00—Components to be removed
    • B01D2257/30—Sulfur compounds
    • B01D2257/302—Sulfur oxides
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2257/00—Components to be removed
    • B01D2257/40—Nitrogen compounds
    • B01D2257/404—Nitrogen oxides other than dinitrogen oxide
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2258/00—Sources of waste gases
    • B01D2258/02—Other waste gases
    • B01D2258/0283—Flue gases
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2259/00—Type of treatment
    • B01D2259/40—Further details for adsorption processes and devices
    • B01D2259/40003—Methods relating to valve switching
    • B01D2259/40005—Methods relating to valve switching using rotary valves
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2259/00—Type of treatment
    • B01D2259/40—Further details for adsorption processes and devices
    • B01D2259/40011—Methods relating to the process cycle in pressure or temperature swing adsorption
    • B01D2259/40077—Direction of flow
    • B01D2259/40081—Counter-current
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2259/00—Type of treatment
    • B01D2259/40—Further details for adsorption processes and devices
    • B01D2259/402—Further details for adsorption processes and devices using two beds
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/02—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography
    • B01D53/04—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography with stationary adsorbents
    • B01D53/0407—Constructional details of adsorbing systems
    • B01D53/0446—Means for feeding or distributing gases
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
    • Y02A50/00—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE in human health protection, e.g. against extreme weather
    • Y02A50/20—Air quality improvement or preservation, e.g. vehicle emission control or emission reduction by using catalytic converters

Definitions

  • This invention relates to an improved process for desulfurization and denitrification of a waste gas containing sulfur oxides, nitrogen oxides and halogen-containing materials such as hydrogen chloride, hydrogen fluoride, etc., more specifically a waste gas from combustion of coal, containing relatively large amounts of halogens, for example, about several ppm to 200 ppm of halogen components.
  • the desulfurization and denitrification technique using a carbonaceous adsorbent consists of a method comprising passing a waste gas transversely through a reactor of a moving bed type wherein a carbonaceous adsorbent is vertically moved from the upper part to the lower part, whereby sulfur oxides are adsorbed and removed and nitrogen oxides are decomposed and removed by the aid of ammonia.
  • a gas processing apparatus comprising a reactor consisting of a first moving bed and second moving bed, connected in series, in which a carbonaceous adsorbent is moved from the upper part to the lower part, and to effect mainly desulfurization by firstly feeding a waste gas to the first moving bed and passing the waste gas transversely through the carbonaceous adsorbent layer, and then mainly denitrification by adding ammonia to the waste gas passed through the first moving bed, feeding to the second moving bed and passing the waste gas transversely through the carbonaceous adsorbent layer.
  • the carbonaceous adsorbent is firstly fed to the second moving bed, subjected to denitrification reaction, then fed to the first moving bed to adsorb sulfur oxides and the carbonaceous adsorbent whose activity is lowered by the adsorption of sulfur oxides in the form of sulfuric acid or ammonium salt is discharged from the reactor, followed by subjecting to regeneration and reusing.
  • these halogen-containing materials are more difficult to be adsorbed on a carbonaceous adsorbent as compared with sulfur oxides and accordingly, when the concentration of sulfur oxides is high and the adsorption capacity of the carbonaceous adsorbent is not sufficient, or when a processing operation is carried out under such a condition that movement of the carbonaceous adsorbent is controlled to adsorb sulfur oxides up to near the saturation adsorption quantity, the halogen-containing materials are hardly adsorbed and are passed through the first moving bed, followed by reacting with ammonia gas added between the first moving bed and the second moving bed to form ammonium halides, entering the second moving bed with the waste gas and adsorbing on the carbonaceous adsorbent in the second moving bed.
  • the carbonaceous adsorbent, on which ammonium halides have been adsorbed, is moved downward in the moving bed and fed to the first moving bed.
  • the ammonium halide-adsorbing carbonaceous adsorbent is contacted with a waste gas containing a large amount of sulfur oxides in the first moving bed, the sulfur oxides and ammonium halides are reacted to form ammonium sulfate and ammonium sulfite and to again generate hydrogen halide gases. That is, the halogen-containing materials contained in the waste gas are cycled and gradually accumulated between the first moving bed and the second moving bed.
  • the concentration of halogens is increased in the gas fed from the first moving bed to the second moving bed, the amount of ammonium halides formed by addition of ammonia gas is increased and the ammonium halides are adsorbed in large amounts on the carbonaceous adsorbent in the second moving bed, in particular, on the carbonaceous adsorbent at the gas inlet side, causing problems of increase of the pressure loss and clogging of an inlet louver.
  • a process for the desulfurization and denitrification of a waste gas containing halogen-containing materials in addition to SOx and NOx comprising using a gas-processing apparatus consisting of a first moving bed and a second moving bed in which a carbonaceous adsorbent is moved from the upper part to the lower part, firstly feeding the waste gas to the first moving bed and passing it transversely through the carbonaceous adsorbent where desulfurization is mainly carried out, then adding ammonia to the waste gas having passed through the first moving bed, feeding it to the second moving bed and passing it transversely through the carbonaceous adsorbent where denitrification is mainly carried out, while feeding the carbonaceous adsorbent firstly to the second moving bed where the carbonaceous adsorbent is subjected to denitrification, then feeding the carbonaceous adsorbent to the first moving bed where the carbonaceous adsorbent is subjected to adsorption of sulfur oxides
  • FIG. 1 is a schematic view of one embodiment of an apparatus for the desulfurization and denitrification according to the present invention.
  • FIG. 2 is a schematic view of an apparatus for the desulfurization and denitrification according to the prior art.
  • the inventor has made various efforts to improve a moving bed reactor for the desulfurization and denitrification of a waste gas and consequently, reached the present invention relating to the moving bed reactor for the desulfurization and denitrification of a waste gas, in particular, containing halogen-containing materials in addition to SOx and NOx.
  • FIG. 1 is a schematic view of a preferred embodiment of the present invention
  • FIG. 2 is a schematic view of a desulfurization and denitrification apparatus of the prior art.
  • a desulfurization and denitrification apparatus 1 is composed of a first moving bed 2 for mainly effecting desulfurization and a second moving bed 3 for mainly effecting denitrification.
  • a waste gas is first fed to the first moving bed 2 via a waste gas inlet 4, contacted transversely with a carbonaceous adsorbent, introduced into the apparatus 1 through adsorbent feed port 7, moving from the upper part to the lower part in the apparatus to adsorb and remove the most part of sulfur oxides, and then fed to the second moving bed 3 through a gas path 5, during which ammonia is added to the waste gas from an ammonia feed port 9.
  • This ammonia-containing waste gas is transversely contacted with the carbonaceous adsorbent in the second moving bed, where nitrogen oxides are decomposed and removed by the action of the carbonaceous adsorbent and ammonia and the residual sulfur oxides are also adsorbed and removed to render them harmless, and then discharged to outside the system from a waste gas outlet 6.
  • an apparatus comprising a first moving bed and a second moving bed in which a carbonaceous adsorbent is moved from the second moving bed to the first moving bed, louver units provided at both the sides of the first and second moving beds for holding the carbonaceous adsorbent moving downward, a gas-permeable partition plate provided in parallel with the flow of the carbonaceous adsorbent in the second moving bed to divide the bed of the adsorbent into a bed at the inlet side of the waste gas and another bed at the outlet side, the carbonaceous adsorbent having moved downward in the bed at the outlet side of the waste gas being fed to the first moving bed as it is, and the carbonaceous adsorbent having moved downward in the bed at the inlet side of the waste gas and adsorbed ammonium halides being taken out of the system and subjected to regeneration
  • the quantity of movement of the carbonaceous adsorbent is so controlled, from the standpoint of effective utilization of the carbonaceous adsorbent, that the quantity of adsorption of sulfur oxides substantially reaches the saturation point. Since the adsorption on a carbonaceous adsorbent is anticipated by sulfur oxides more readily being adsorbable, halogen-containing materials such as hydrogen chloride, hydrogen fluoride, etc., contained in a waste gas, are hardly adsorbed thereby and thus are passed through the first moving bed.
  • the concentration of the halogen components is increased in the waste gas, the amount of the ammonium halides formed by the reaction with ammonia gas is also increased and they tend to adhere to a louver 10 at the gas inlet in the second moving bed 3, a sub-louver 11 and the carbonaceous adsorbent flowing at the inlet side, resulting in problems that the pressure loss is increased and clogging takes place.
  • the process of the present invention aims at preventing the halogen components from accumulation in the above described SO x and NO x removal system.
  • the feature of the present invention consists in providing a gas-permeable partition plate 12 inside the inlet louver 10 in the second moving bed 3 to divide the bed of the carbonaceous adsorbent in the second moving bed 3 into a bed (Bed A) at the inlet side of the waste gas and another bed (Bed B) at the outlet side thereof, feeding the carbonaceous adsorbent with a small adsorption amount of ammonium halides, flowing downward in Bed B, to the first moving bed 2 as it is, withdrawing the carbonaceous adsorbent carrying a large amount of ammonium halides, flowing downward in Bed A, out of an adsorbent discharge port 13 to outside the system, combining with the adsorbent leaving an adsorbent discharge port 8 in the first moving bed 2 and then subjecting it to regeneration.
  • the structure of the partition plate 12 is not particularly limited, but any gas-permeable structure can be used such as porous or perforated plates having air holes with various shapes, various grating plates, etc. which are capable of dividing the bed of a carbonaceous adsorbent and have sufficient gas-permeability.
  • the size, structure and installation position of the partition plate 12 can suitably be determined depending on the size of the apparatus and operation conditions such as gas flow rate, concentration of harmful components contained in a gas, etc.
  • a sub-louver is ordinarily provided inside a main louver so as to prevent the louver at the gas inlet from accumulation of the carbonaceous adsorbent thereon.
  • the function of the partition plate according to the present invention can be given to the sub-louver by controlling the position and shape of the sub-louver in such a manner that the carbonaceous adsorbent flowing downward between the main louver and sub-louver can be withdrawn out of the system.
  • the adsorbent discharge port 13 from which the adsorbent carrying a large amount of ammonium halides is withdrawn out of this system without entering the first moving bed 2.
  • the thus withdrawn adsorbent is fed to a regeneration process and regenerated with the adsorbent discharged from the adsorbent dicharge port 8 of the first moving bed 2.
  • the ratio of the carbonaceous adsorbents moving in Beds A and B can suitably be determined by the operation conditions, etc., as described above, but specifically, it can be controlled by the position of the partition plate determined at the time of designing the apparatus, the quantity of an adsorbent supplied, the quanity thereof withdrawn, controlled by a rotary valve connected to the adsorbent discharge port at the lower part of Bed A.
  • the ratio of Bed A and Bed B is in the range of 4:96 to 35:65 by volume.
  • the flow rates of the carbonaceous adsorbent in Bed A and Bed B largely depend upon the operation conditions of the apparatus, e.g. the amount of the carbonaceous adsorbent for the SOx concentration, the amount of halogens and in practice, the flow rate of Bed A is controlled in a suitable range depending on these conditions. Generally, the flow rate of Bed A is in the range of about 0.1 to 5 times as fast as that of Bed B.
  • a gas-processing apparatus consisting of a first moving bed and a second moving bed in which a carbonaceous adsorbent is moved from the upper part to the lower part, firstly feeding the waste gas to the first moving bed and passing it transversely through the carbonaceous absorbent where desulfurization is mainly carried out, then adding ammonia to the waste gas passing through the first moving bed, feeding it to the second moving bed and passing it transversely through the carbonaceous adsorbent where denitrification is mainly carried out, while feeding the carbonaceous adsorbent firstly to the second moving bed where the carbonaceous adsorbent is subjected to denitrification, then feeding the carbonaceous adsorbent to the first moving bed where the carbonaceous adsorbent is subjected to adsorption of sulfur oxides and then
  • test apparatus each comprising a carbonaceous adsorbent and a gas flow path structure, in which two moving beds of the carbonaceous adsorbent were connected in series, as shown in FIGS. 1 and 2, a waste gas from combustion of coal, comprising 875 ppm of SO 2 , 440 ppm of NO x , 30 ppm of HCl and balance of N 2 was subjected to a test to examine the accumulation state of HCl in the gas path 5 and the progress of the pressure loss.
  • the second moving bed of the carbonaceous adsorbent was composed of 10% of Bed A and 90% of Bed B.
  • the partition plate 12 was not provided as in the prior art.

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  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Analytical Chemistry (AREA)
  • General Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Health & Medical Sciences (AREA)
  • Biomedical Technology (AREA)
  • Environmental & Geological Engineering (AREA)
  • Treating Waste Gases (AREA)
  • Separation Of Gases By Adsorption (AREA)
US07/942,829 1991-09-18 1992-09-10 Process for the desulfurization and denitrification of a waste gas containing halogen-containing materials Expired - Lifetime US5294420A (en)

Applications Claiming Priority (4)

Application Number Priority Date Filing Date Title
JP26537191 1991-09-18
JP3-265371 1991-09-18
JP10903892A JP3242443B2 (ja) 1991-09-18 1992-04-03 ハロゲン物質含有排ガスの脱硫脱硝方法
JP4-109038 1992-04-03

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US5294420A true US5294420A (en) 1994-03-15

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US (1) US5294420A (fr)
EP (1) EP0533480A1 (fr)
JP (1) JP3242443B2 (fr)
KR (1) KR930005662A (fr)
CN (1) CN1070588A (fr)
CA (1) CA2078577A1 (fr)

Cited By (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US5527514A (en) * 1993-11-18 1996-06-18 Sumitomo Heavy Industries, Ltd. Desulfurizing and denitrating tower
US5932179A (en) * 1996-10-30 1999-08-03 Sumitomo Heavy Industries, Ltd. Waste gas treatment apparatus
EP0882491A4 (fr) * 1996-10-09 1999-12-15 Sumitomo Heavy Industries Procede de traitement de gaz d'echappement
US20110014767A1 (en) * 2001-12-20 2011-01-20 Ahn Kie Y LOW-TEMPERATURE GROWN HIGH QUALITY ULTRA-THIN CoTiO3 GATE DIELECTRICS
CN111408263A (zh) * 2020-03-20 2020-07-14 北京海顺德钛催化剂有限公司 烟气处理装置
US11571655B2 (en) * 2016-12-29 2023-02-07 Institute Of Process Engineering, Chinese Academy Of Sciences Activated carbon adsorption tower and gas purification device

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JPH07141775A (ja) * 1993-11-18 1995-06-02 Matsushita Electric Ind Co Ltd 記録再生装置
WO1996004065A1 (fr) * 1994-07-29 1996-02-15 Steag Aktiengesellschaft Reacteur a adsorption utilise pour extraire les composants indesirables d'un fluide
CN1331573C (zh) * 2004-12-22 2007-08-15 唐华 间歇式移动床干法脱硫装置及其脱硫方法
DE102005001595A1 (de) * 2005-01-12 2006-07-20 Grochowski, Horst, Dr. Verfahren zum Reinigen von Abgasen eines Glasschmelzprozesses, insbesondere für Gläser für LCD-Bildschirme
US7776293B2 (en) * 2007-08-02 2010-08-17 Babcock & Wilcox Power Generation Group, Inc. Low-temperature, moving bed catalytic reactor for control of NOx emissions from combustion
JP5440969B2 (ja) * 2007-08-03 2014-03-12 千明 武内 半湿式吸着剤脱臭法
JP4695126B2 (ja) * 2007-09-20 2011-06-08 ジェイパワー・エンテック株式会社 排ガスの脱硫脱硝装置
CN101785953B (zh) * 2010-03-19 2012-02-22 东南大学 利用错流移动床去除水泥窑炉烟气中有害成分的装置及方法
CN106693603B (zh) * 2015-11-13 2023-05-09 中冶长天国际工程有限责任公司 活性炭法烟气净化装置及烟气净化方法
KR101671670B1 (ko) 2016-05-09 2016-11-01 신경재 드레인장치 및 이를 구비한 열교환기
CN106016292B (zh) * 2016-07-04 2018-07-10 陈仕敏 一种旋流沉降罐及无烟雾垃圾焚烧系统
CN110465185A (zh) * 2018-05-10 2019-11-19 襄阳先天下环保设备有限公司 一种催化法脱硫制硫酸设备
KR102877555B1 (ko) 2022-11-30 2025-10-27 재단법인 포항산업과학연구원 활성 코크스의 제조방법 및 이를 이용하여 제조된 활성 코크스

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US2992895A (en) * 1957-08-28 1961-07-18 Reinluft Ges M B H Fa Process for recovering oxides of nitrogen and sulfur from gaseous mixtures
US4272497A (en) * 1979-02-08 1981-06-09 Sumitomo Heavy Industries, Ltd. Method for treating a nitrogen oxide- and sulphur oxide-containing waste gas
US4500501A (en) * 1981-09-10 1985-02-19 Mitsui Mining Company Ltd. Method of removing sulfur oxides and nitrogen oxides by dry process
US4741884A (en) * 1981-11-13 1988-05-03 Phillips Petroleum Company Process and apparatus for removing H2 S from gas streams
US4789531A (en) * 1985-06-29 1988-12-06 Steag Aktiengesellschaft Method of removing nitrogen oxides (NOx) from gases, especially flue gases
US5053210A (en) * 1986-02-11 1991-10-01 Uhde Gmbh Method for the purification of flue gases

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US4670226A (en) * 1985-04-15 1987-06-02 Mitsui Mining Company, Limited Reactor of moving bed type
DE3917271A1 (de) * 1989-05-24 1990-11-29 Siemens Ag Verfahren zur entfernung von schwefeloxiden und stickstoffoxiden aus rauchgasen

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Publication number Priority date Publication date Assignee Title
US2992895A (en) * 1957-08-28 1961-07-18 Reinluft Ges M B H Fa Process for recovering oxides of nitrogen and sulfur from gaseous mixtures
US4272497A (en) * 1979-02-08 1981-06-09 Sumitomo Heavy Industries, Ltd. Method for treating a nitrogen oxide- and sulphur oxide-containing waste gas
US4500501A (en) * 1981-09-10 1985-02-19 Mitsui Mining Company Ltd. Method of removing sulfur oxides and nitrogen oxides by dry process
US4741884A (en) * 1981-11-13 1988-05-03 Phillips Petroleum Company Process and apparatus for removing H2 S from gas streams
US4789531A (en) * 1985-06-29 1988-12-06 Steag Aktiengesellschaft Method of removing nitrogen oxides (NOx) from gases, especially flue gases
US5053210A (en) * 1986-02-11 1991-10-01 Uhde Gmbh Method for the purification of flue gases

Cited By (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US5527514A (en) * 1993-11-18 1996-06-18 Sumitomo Heavy Industries, Ltd. Desulfurizing and denitrating tower
EP0882491A4 (fr) * 1996-10-09 1999-12-15 Sumitomo Heavy Industries Procede de traitement de gaz d'echappement
US5932179A (en) * 1996-10-30 1999-08-03 Sumitomo Heavy Industries, Ltd. Waste gas treatment apparatus
AU720010B2 (en) * 1996-10-30 2000-05-18 Sumitomo Heavy Industries Ltd. Waste gas treatment apparatus
US20110014767A1 (en) * 2001-12-20 2011-01-20 Ahn Kie Y LOW-TEMPERATURE GROWN HIGH QUALITY ULTRA-THIN CoTiO3 GATE DIELECTRICS
US11571655B2 (en) * 2016-12-29 2023-02-07 Institute Of Process Engineering, Chinese Academy Of Sciences Activated carbon adsorption tower and gas purification device
CN111408263A (zh) * 2020-03-20 2020-07-14 北京海顺德钛催化剂有限公司 烟气处理装置

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